Process for the production of chlorinated alkanes

ABSTRACT

Processes for the production of chlorinated alkanes are provided. The present processes comprise catalyzing the chlorination of a feedstream comprising one or more alkanes and/or alkenes with a catalyst system comprising one or more inorganic iodine salts and/or lower than conventional levels of elemental iodine and at least one Lewis acid. The processes are conducted in a nonaqueous media, and so, the one or more inorganic iodine salts are recoverable and/or reusable, in whole or in part.

The present invention relates to processes for the production of chlorinated alkanes in a nonaqueous media.

BACKGROUND

Hydrofluorocarbon (HFC) products are widely utilized in many applications, including refrigeration, air conditioning, foam expansion, and as propellants for aerosol products including medical aerosol devices. Although HFC's have proven to be more climate friendly than the chlorofluorocarbon and hydrochlorofluorocarbon products that they replaced, it has now been discovered that they exhibit an appreciable global warming potential (GWP).

The search for more acceptable alternatives to current fluorocarbon products has led to the emergence of hydrofluoro-olefin (HFO) products. Relative to their predecessors, HFOs are expected to exert less impact on the atmosphere in the form of a lesser, or no, detrimental impact on the ozone layer and their lower GWP as compared to HFC's. Advantageously, HFO's also exhibit low flammability and low toxicity.

As the environmental, and thus, economic importance of HFO's has developed, so has the demand for precursors utilized in their production. Many desirable HFO compounds, e.g., such as 2,3,3,3-tetrafluoroprop-1-ene or 1,3,3,3-tetrafluoroprop-1-ene, may typically be produced utilizing feedstocks of chlorocarbons, and in particular, highly chlorinated alkanes, e.g., tetra- and pentachloroalkanes.

Unfortunately, these higher chlorides have proven difficult to manufacture using acceptable process conditions and in commercially acceptable regioselectivities and yields. For example, conventional processes for the production of pentachloropropanes provide unacceptable selectivity to the desired pentachloropropane isomer(s), i.e., 1,1,2,2,3-pentachloropropane, make use of suboptimal chlorinating agents, require the use of high intensity process conditions and/or catalyst systems that are difficult to utilize in large scale production processes and/or are wholly or partly unrecoverable or otherwise unreusable.

It would thus be desirable to provide improved processes for the production of chlorocarbon precursors useful as feedstocks in the synthesis of refrigerants and other commercial products. More particularly, such processes would provide an improvement over the current state of the art if they provided a higher regioselectivity relative to conventional methods, made use of optimal chlorinating agents, required low intensity process conditions, made use of catalyst systems and/or initiators more amenable to use in large-scale processes, such as those that may be recovered or otherwise reused.

BRIEF DESCRIPTION

The present invention provides efficient processes for the production of highly chlorinated alkanes. More particularly, the processes make use of one or more inorganic iodine salts, or other inorganic precursors to at least one hypervalent iodine species, and/or low levels of elemental iodine desirably as part of a mixed catalyst system further comprising at least one Lewis acid. The use of inorganic iodine salts is advantageous as compared to conventional processes, in that inorganic iodine salts are not as corrosive or volatile as elemental iodine when employed at conventional levels, and so, are more readily and conveniently incorporated into large scale manufacturing process. Because the present processes are desirably conducted in a nonaqueous media, the inorganic iodine salts are recoverable and/or reusable, providing significant cost savings to the process. Further cost savings are provided in that low intensity process conditions, e.g., low temperatures, ambient pressure and minimal reactor residence time, are utilized.

In one aspect, the present invention provides a process for the production of chlorinated alkanes. The process comprises catalyzing the chlorination of a feedstream comprising one or more alkanes and/or alkenes in a nonaqueous media with a mixed catalyst system comprising one or more inorganic iodine salts, and/or less than 10,000 ppm elemental iodine and at least one Lewis acid. Although an inorganic iodine salt is used as part of the catalyst system, and in some advantageous embodiments, no iodine is added to the starting alkane and/or alkene. In some embodiments, the one or more inorganic iodine salts may comprise hypoiodites (IO⁻), iodites (IO²⁻), iodates IO³⁻, and/or periodates (IO⁴⁻), including metaperiodates and orthoperiodates, or combinations of these. In some embodiments, the concentration of elemental iodine used, if any, may be from 1 ppm to 5000 ppm, or from 5 ppm to 1000 ppm, or from 10 ppm to 100 ppm. The source of chlorine atoms may comprise chlorine gas, sulfuryl chloride or a combination of these, and in some embodiments comprises sulfuryl chloride, which may also act as a diluent or solvent as well as a chlorine source. The alkane and/or alkene may initially be unchlorinated, or, may already comprise chlorine atoms, and may comprise any number of carbon atoms.

DETAILED DESCRIPTION

The present specification provides certain definitions and methods to better define the present invention and to guide those of ordinary skill in the art in the practice of the present invention. Provision, or lack of the provision, of a definition for a particular term or phrase is not meant to imply any particular importance, or lack thereof. Rather, and unless otherwise noted, terms are to be understood according to conventional usage by those of ordinary skill in the relevant art.

The terms “first”, “second”, and the like, as used herein do not denote any order, quantity, or importance, but rather are used to distinguish one element from another. Also, the terms “a” and “an” do not denote a limitation of quantity, but rather denote the presence of at least one of the referenced item, and the terms “front”, “back”, “bottom”, and/or “top”, unless otherwise noted, are merely used for convenience of description, and are not limited to any one position or spatial orientation.

If ranges are disclosed, the endpoints of all ranges directed to the same component or property are inclusive and independently combinable (e.g., ranges of “up to 25 wt. %, or, more specifically, 5 wt. % to 20 wt. %,” is inclusive of the endpoints and all intermediate values of the ranges of “5 wt. % to 25 wt. %,” etc.). As used herein, percent (%) conversion is meant to indicate change in molar or mass flow of reactant in a reactor in ratio to the incoming flow, while percent (%) selectivity means the change in molar flow rate of product in a reactor in ratio to the change of molar flow rate of a reactant.

Reference throughout the specification to “one embodiment” or “an embodiment” means that a particular feature, structure, or characteristic described in connection with an embodiment is included in at least one embodiment. Thus, the appearance of the phrases “in one embodiment” or “in an embodiment” in various places throughout the specification is not necessarily referring to the same embodiment. Further, the particular features, structures or characteristics may be combined in any suitable manner in one or more embodiments.

As used herein, the term “inorganic iodine salt” is meant to include any inorganic salt, incorporating, or otherwise capable of providing or forming in a reaction mixture, at least one hypervalent iodine species. Typically, such compounds may further be characterized in that they comprise at least metal and iodine elements. The term “hypervalent”, in turn, refers to iodine sources having oxidation states of greater than or equal to +1, e.g., +1, +3, +5, +7, etc.

The present invention provides efficient processes for the production of chlorinated alkanes. The present processes catalyze the chlorination of a feedstream comprising one or more alkanes and/or alkenes with one or more inorganic iodine salt and at least one Lewis acid. Further, the processes take place in a nonaqueous media, and as a result, the one or more inorganic iodine salts may be recovered in whole or in part, and/or reused. The use of an inorganic iodine salt is further advantageous in that inorganic iodine salts do not present the volatility and corrosion issues that can be presented by elemental iodine when used at conventional levels, as is used in conventional processes for the production of chlorinated alkanes.

Any inorganic iodine salt can be used in the mixed catalyst system, and those of ordinary skill in the art are expected to be familiar with many. Suitable examples include, but are not limited to, hypoiodites (IO⁻), iodites (IO²⁻), iodates (IO³⁻), and/or periodates (IO⁴⁻), including mesoperiodates and orthoperiodates, or combinations of these. Specific examples of inorganic iodine salts include, but are not limited to sodium iodate, silver iodate, calcium iodate, potassium iodate, iodic acid, sodium periodate, potassium periodate, barium periodate, and periodic acid, and derivatives or combinations of any number of these.

In other embodiments, elemental iodine may be used, but at levels much lower than previously thought to be effective. That is, it has now been discovered that amounts of iodine much lower than conventionally utilized, e.g., 0.01 wt %, provide improvements in yield and selectivity while yet not presenting the corrosion and volatility issues that may arise when these conventional levels are utilized. More specifically, amounts of elemental iodine of from 1 ppm to 5000 ppm, or from 5 ppm to 1000 ppm, or from 10 ppm to 100 ppm, have now surprisingly been discovered to provide selectivities to the desired chloropropanes of greater than 60%, in some cases greater than 70%, and in some cases greater than 80%. This is a significant improvement over processes wherein no iodine is used at all, wherein conversions of e.g., less than 60% can be seen. Since elemental iodine can be costly, significant cost savings are also provided by using the smaller amounts described herein. Combinations of one or more inorganic iodine salts and elemental iodine may also be used.

The mixed catalyst system used in the process also desirably comprises at least one Lewis acid. Any Lewis acid that at least marginally enhances the process can be utilized, and examples of these include, but are not limited to ferric chloride, antimony pentafluoride, boron trichloride, aluminum trichloride, and stannic chloride. Combinations of two or more of these may also be used, if desired. In some embodiments, anhydrous aluminum chloride may desirably be utilized as the at least one Lewis acid.

Generally speaking, enough of the mixed catalyst system should be utilized to provide some improvement to reaction process conditions (e.g., a reduction in required temperature) and desirably, reaction selectivity, but yet not be more than will provide any additional benefit, if only for reasons of economic practicality. For purposes of illustration only, then, it is expected that useful concentrations of the inorganic iodine salt, in a batch process, will range from 0.01% to 30% by weight with respect to the alkane and/or alkene, or from 0.1% to 20%, or from 1% to 10 wt %, inclusive of all subranges therebetween. Surprisingly low levels of elemental iodine are effective, e.g., from 1 ppm to 5000 ppm, or from 5 ppm to 1000 ppm, or from 10 ppm to 100 ppm. Suitable amounts of the Lewis acid will range from 0.01% to 20% by weight each with respect to the dichlorinated alkane, or from 0.1% to 10%, or from 1% to 5 wt %, inclusive of all subranges therebetween. For continuous processes, it is possible that much lower concentrations, e.g., as much as 5, or 10, or 15 or even 20 times lower will not only be effective, but be effective over the entire course of plant operability.

The chlorine atoms are desirably supplied by chlorine gas, sulfuryl chloride, or both. Sulfuryl chloride (SO₂Cl₂), can also act as a solvent for the mixed catalyst systems and/or reactions, thereby assisting in the provision of an acceptable reaction rate and/or yield. And so, in some embodiments, sulfuryl chloride may desirably be used as the chlorinating agent.

In some embodiments, including those wherein chlorine is used as a chlorinating agent rather than sulfuryl chloride, a solvent may be used in the present processes. Desirably, any solvent will be inert to the desired chemistry, allow for adequate mass transfer during the chemical reaction, and create a homogenous phase to insure uniform reactivity throughout the reactor. Chlorocarbon solvents are especially well suited for the present processes due to their ease in handling and relative resistance to the desired chemistry, and many of these are known to those of ordinary skill in the art. For example, suitable chlorocarbon solvents include, but are not limited to carbon tetrachloride, methylene chloride, chloroform, 1,2,3-trichloropropane, 1,1,2,3-tetrachloropropane, and 1,1,2,2,3,3-hexachloropropane. In some embodiments, the chlorocarbon solvent may comprise methylene chloride or 1,2,3-trichloropropane.

The reaction conditions under which the process is carried out are advantageously low intensity. That is, low temperatures, e.g., of less than 100° C., or less than 90° C., or less than 80° C. or less than 70° C., or less than 60° C., may be utilized and the desired selectivities to the desired chlorinated alkanes yet be realized. In some embodiments, temperatures of from 40° C. to 90° C., or from 50° C. to 80° C., or from 55° C. to 75° C. may be utilized. Similarly, ambient pressure is suitable for carrying out the process, or pressures within 250, or 200, or 150, or 100, or 50, or 40, or 30, or 20, or even 10 psi, of ambient are suitable. Reactor occupancy may also be minimized with the desired selectivities yet seen—for example, reactor occupancy times of less than 20 hours, or less than 15 hours, or less than 10 hours, or less than 9, 8, 7, 6, or even 5 hours, are possible. The reactor may be any suitable liquid phase reactor, such as a batch or continuous stirred tank autoclave reactor with an internal cooling coil. A shell and multitube exchanger followed by vapor liquid disengagement tank or vessel can also be used.

The present process can make use of one or more alkanes or alkenes to produce the desired chlorinated alkanes. Alkanes or alkenes having any number of carbon atoms and that are desirably chlorinated in a nonaqueous media may benefit from application of the present process. Generally speaking, alkanes or alkenes comprising from 2-10 carbon atoms, or from 2-8 carbon atoms, or from 2-6 carbon atoms, or from 2-5 carbon atoms, or from 2-4 carbon atoms, are particularly suitable. In some embodiments, the alkane or alkene may comprise a propane or propene.

Similarly, the alkane and or alkene may be unchlorinated, or may comprise chlorine atoms prior to application of the process. That is, the alkane and/or alkene may comprise any number of chlorine atoms, including zero. To some degree, the number of chlorine atoms in the alkane or alkene will be limited by the number of carbon atoms, as well as the chlorinated alkane desirably produced. In some embodiments, the alkane and/or alkene may comprise from 0-4 chlorine atoms, or may comprise 1-3 chlorine atoms. In some embodiments, the alkane and/or alkene may be a mono-, di-, or trichlorinated propane, such as 1- or 2-chloropropane, 1,2-dichlorinated propane, and/or 1,1,2-trichlorinated propane.

The chlorinated alkane produced by the process will depend upon the alkane and/or alkene used as a starting material, and so, in some embodiments, and due to the commercial significance of trichlorinated alkanes having three to six carbon atoms, the use of one or more propanes, propenes, butanes, butenes, pentanes, pentenes, hexanes and hexanes as starting materials may be preferred.

In one exemplary process, a dichloropropane, e.g., 1,2-dichloropropane, is utilized as a starting material and reacted with sulfuryl chloride in the presence of sodium iodate at a temperature of from 55° C. to 75° C., ambient pressure and a reactor occupancy of less than five hours to produce a pentachloropropane, e.g., 1,1,2,2,3-pentachloropropane at regioselectivities of greater than 10:1, or greater than 20:1 or greater than 30:1, or even greater than 40:1, over other pentachloropropane products.

Some embodiments of the invention will now be described in detail in the following examples.

EXAMPLE 1 Chlorination of 1,2-dichloropropane to 1,1,2,2,3-pentachloropropane Using Sodium Periodate as Inorganic Iodine Salt, Aluminum Chloride as Lewis acid and Sulfuryl Chloride as Chlorinating Agent

17 g sulfuryl chloride and 2.5 g aluminum chloride is charged to a reactor equipped with a magnetic stir bar and reflux condenser. The reaction mixture is heated to 60° C. and then 4.1 g of 1,2-dichloropropane is charged. The reaction is allowed to stir for 35 minutes, where GC analysis indicated that >99% of the 1,2-dichloropropane had been reacted to form primarily 1,1,2-trichloropropane.

An additional 15 g of sulfuryl chloride along with 1 g of sodium periodate is added. The reaction is allowed to react for a total 4 hours before being cooled back to ambient temperature. The crude reaction mixture is filtered to collect the sodium periodate catalyst as a wet cake that is washed with methylene chloride to give 0.8 g of recovered sodium periodate.

The reaction mixture and methylene chloride wash are combined, slowly poured into an ice water bath, and allowed to stir until quenched. The organic and aqueous phases are separated and the aqueous phase is extracted with an equal volume of methylene chloride. The combined organic fractions are dried over magnesium sulfate, the excess solvent is removed by rotary evaporator, and the final product is isolated as a colored oil.

GC and NMR analysis of the final product mixture shows a yield of 4.7 g of 1,1,2,2,3-pentachloropropane, 0.7 g of tetrachloropropane isomers, 0.4 g of 1,1,2-trichloropropane, 0.3 g of hexachloropropane isomers, and 0.2 g of 1,2,3-trichloropropane.

EXAMPLE 2 Chlorination of 1,2-dichloropropane to 1,1,2,2,3-pentachloropropane Using Recovered Sodium Periodate as Inorganic Iodine Salt, Aluminum Chloride as Lewis Acid and Sulfuryl Chloride as Chlorinating Agent

9.3 g sulfuryl chloride and 1.3 g aluminum chloride is charged to a reactor equipped with a magnetic stir bar and reflux condenser. The reaction mixture is heated to 60° C. and charged with 2.3 g of 1,2-dichloropropane. The reaction is allowed to stir for 35 minutes, when GC analysis indicates that >99% of the 1,2-dichloropropane has reacted to form primarily 1,1,2-trichloropropane.

An additional 7.9 g of sulfuryl chloride along with 0.5 g of sodium periodate recovered from Example 1 is charged. The reaction is allowed to react for a total 4 hours before being cooled back to ambient temperature. The crude reaction mixture is filtered to collect the sodium periodate catalyst as a wet cake that is washed with methylene chloride to give 0.45 g of recovered sodium periodate.

The reaction mixture and methylene chloride wash are combined, slowly poured into an ice water bath, and allowed to stir until quenched. The organic and aqueous phases are separated and the aqueous phase is extracted with an equal volume of methylene chloride. The combined organic fractions are dried over magnesium sulfate, the excess solvent is removed by rotary evaporator, and the final product is isolated as a colored oil.

GC and NMR analysis of the final product mixture shows a yield of 3.1 g of 1,1,2,2,3-pentachloropropane, 0.5 g of hexachloropropane isomers, 0.1 g of 1,2,3-trichloropropane, and 0.1 g of tetrachloropropane isomers.

EXAMPLE 3 Chlorination of 1,2-dichloropropane to 1,1,2,2,3-pentachloropropane Using Sodium Iodate as Inorganic Iodine Salt, Aluminum Chloride as Lewis acid and Sulfuryl Chloride as Chlorinating Agent

17 g sulfuryl chloride and 2.5 g aluminum chloride is charged to a reactor equipped with a magnetic stir bar and reflux condenser. The reaction mixture is heated to 60° C. and then 4.1 g of 1,2-dichloropropane is charged. The reaction is allowed to stir for 35 minutes, when GC analysis indicates that >99% of the 1,2-dichloropropane has reacted to form primarily 1,1,2-trichloropropane.

An additional 15 g of sulfuryl chloride along with 0.5 g of sodium iodate is charged. The reaction is allowed to react for a total 4 hours before being cooled back to ambient temperature. The reaction mixture is slowly poured into an ice water bath and allowed to stir until quenched. The organic and aqueous phases are separated and the aqueous phase is extracted with an equal volume of methylene chloride. The sodium iodate is recovered in the aqueous wash as indicated by ion chromatography analysis. The combined organic fractions are dried over magnesium sulfate, the excess solvent is removed by rotary evaporator, and the final product was isolated as a colored oil.

GC and NMR analysis of the final product mixture shows a yield of 5.4 g of 1,1,2,2,3-pentachloropropane, 0.6 g of tetrachloropropane isomers, 0.4 g of hexachloropropane isomers, 0.3 g of 1,1,2-trichloropropane and 0.2 g of 1,2,3-trichloropropane.

EXAMPLE 4 Chlorination of 1,2-dichloropropane to 1,1,2,2,3-pentachloropropane Using Sodium Iodate as Inorganic Iodine Salt, Aluminum Chloride as Lewis Acid and Sulfuryl Chloride as Chlorinating Agent

17 g sulfuryl chloride, 0.6 g aluminum chloride, and 0.8 g of sodium iodate is charged to a reactor equipped with a magnetic stir bar and reflux condenser. The reaction mixture is heated to 60° C. and then 4.1 g of 1,2-dichloropropane is added. The reaction is allowed to stir for a total 4 hours before being cooled back to ambient temperature.

The reaction mixture is slowly poured into an ice water bath and allowed to stir until quenched. The organic and aqueous phases are separated and the aqueous phase is extracted with an equal volume of methylene chloride. The sodium iodate is recovered in the aqueous wash as indicated by ion chromatography analysis. The combined organic fractions are dried over magnesium sulfate, the excess solvent is removed by rotary evaporator, and the final product is isolated as a colored oil.

GC and NMR analysis of the final product mixture shows a yield of 2.3 g of 1,1,2,2,3-pentachloropropane, 1.4 g of 1,1,2-trichloropropane, 0.9 g of tetrachloropropane isomers, 0.8 g of 1,2,3-trichloropropane, and 0.2 g of hexachloropropane isomers.

EXAMPLE 5 Chlorination of 1,1,2-trichloropropane to 1,1,2,2,3-pentachloropropane Using Low Levels of Elemental Iodine, Aluminum Chloride as Lewis Acid, Chlorine as Chlorinating Agent, and Methylene Chloride as Chlorocarbon Solvent

A product stream is prepared by feeding chlorine gas at 30 sccm through a starting mixture of 22.6 wt % 1,2-dichloropropane, 1.3 wt % aluminum chloride, and 76.1 wt % methylene chloride at 130 psig and 70° C. until GC analysis indicates that the starting dichloropropane has undergone 68% conversion to give 1,1,2-trichloropropane as the major intermediate species. This stream is charged with 35 ppm elemental iodine dissolved in 15 mL of methylene chloride based on initial dichloropropane within the reaction mixture. The resulting mixture is allowed to stir until 36.1% conversion of the 1,1,2-trichloropropane intermediate is observed to give the desired pentachloropropane and its precursors (can we identify these please?) in 82.3% selectivity over the undesired byproducts of 1,1,2,2,3,3-hexachloropropane and 1,1,2,3-tetrachloropropane. When viewed in light of Example 6, this example shows that virtually the same conversion of 1,1,2-trichloropropane with virtually the same selectivity to the desired pentachloropropane when a significantly lower amount of elemental iodine is used than is conventional. When viewed in combination with Example 7, this example shows that even these low levels of iodine result in significantly greater selectivities to the desired pentachloropropanes than no elemental iodine at all.

EXAMPLE 6 Chlorination of 1,1,2-trichloropropane to 1,1,2,2,3-pentachloropropane Using Conventional Levels of Iodine, Aluminum Chloride as Lewis Acid, Chlorine as Chlorinating Agent, and Methylene Chloride as Inert Chlorocarbon Solvent

A product stream is prepared by feeding chlorine gas at 30 sccm through a starting mixture of 22.6 wt % 1,2-dichloropropane, 1.3 wt % aluminum chloride, and 76.1 wt % methylene chloride at 130 psig and 70° C. until GC analysis indicates that the starting dichloropropane has undergone 69.7 wt % conversion to give 1,1,2-trichloropropane as the major intermediate species. This stream is charged with 0.57 wt % elemental iodine dissolved in 15 mL of methylene chloride based on initial dichloropropane within the reaction mixture. The resulting mixture is allowed to stir until 33.0% conversion of the 1,1,2-trichloropropane intermediate is observed to give the desired pentachloropropane and its precursors in 85.4% selectivity over the undesired byproducts of 1,1,2,2,3,3-hexachloropropane and 1,1,2,3-tetrachloropropane.

EXAMPLE 7 Chlorination of 1,1,2-trichloropropane to 1,1,2,2,3-pentachloropropane in the Absence of Elemental Iodine Using Aluminum Chloride as Lewis Acid, Chlorine as Chlorinating Agent, and Methylene Chloride as Inert Chlorocarbon Solvent

A product stream is prepared by feeding chlorine gas at 30 sccm through a starting mixture of 22.6 wt % 1,2-dichloropropane, 1.3 wt % aluminum chloride, and 76.1 wt % methylene chloride at 130 psig and 70° C. until GC analysis indicates that the starting dichloropropane has undergone 71.5 wt % conversion to give 1,1,2-trichloropropane as the major intermediate species. This stream is charged with 15 mL of methylene chloride. The resulting mixture is allowed to stir until 28.3% conversion of the 1,1,2-trichloropropane intermediate is observed to give the desired pentachloropropane and its precursors in 53.9% selectivity over the undesired byproducts of 1,1,2,2,3,3-hexachloropropane and 1,1,2,3-tetrachloropropane. 

1. A process for the production of chlorinated alkanes comprising, in a nonaqueous media, catalyzing the chlorination of a feedstream comprising one or more alkanes and/or alkenes with a mixed catalyst system comprising one or more inorganic iodine salts and/or less than 10,000 ppm elemental iodine and at least one Lewis acid.
 2. The process of claim 1, wherein the source of chlorine atoms comprises chlorine gas, sulfuryl chloride or a combination of these.
 3. The process of claim 1, wherein the Lewis acid comprises aluminum chloride.
 4. The process of claim 1, wherein the process is conducted in the presence of a chlorocarbon solvent.
 5. The process of claim 1, wherein the alkane and/or alkene comprises from 0-4 chlorine atoms.
 6. The process of claim 5, wherein the alkane and/or alkene is a trichloroalkane or trichloroalkene.
 7. The process of claim 1, wherein the alkane or alkene comprises from 2-6 carbon atoms.
 8. The process of claim 6, wherein the alkane or alkene comprises propane or propene.
 9. The process of claim 1, wherein the chlorinated alkane comprises from 2-6 chlorine atoms.
 10. The process of claim 9, wherein the chlorinated alkane comprises a pentachloropropane.
 11. The process of claim 10, wherein the chlorinated alkane comprises 1,1,2,2,3-pentachloropropane.
 12. The process of claim 1, wherein the inorganic iodine salt is recovered from the process.
 13. The process of claim 1, wherein the inorganic iodine salt comprises one or more hypoiodites, iodites, iodates, periodates, or combinations of these.
 14. The process of claim 13, wherein the inorganic iodine salt comprises sodium iodate, silver iodate, calcium iodate, potassium iodate, iodic acid, sodium periodate, potassium periodate, barium periodate, periodic acid, or derivatives or combinations of any number of these.
 15. The process of claim 14, wherein the inorganic iodine salt comprises sodium iodate, potassium iodiate, sodium periodate, or combinations of these. 